CN207929188U - fluidized bed reactor - Google Patents
fluidized bed reactor Download PDFInfo
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- CN207929188U CN207929188U CN201820188715.8U CN201820188715U CN207929188U CN 207929188 U CN207929188 U CN 207929188U CN 201820188715 U CN201820188715 U CN 201820188715U CN 207929188 U CN207929188 U CN 207929188U
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Abstract
The utility model is related to ebullated bed technical fields, more particularly to a kind of fluidized bed reactor, including reactor shell, three phase separator is arranged in upside inside reactor shell, gas-liquid allotter is arranged in downside inside reactor shell, the gas-liquid allotter includes material distribution pipe, upper tower tray and lower tower tray, upper tower tray and lower tower tray form the double-deck tray structure, gap is formed between upper tower tray and lower tower tray, material distribution pipe runs through upper tower tray and lower tower tray, calotte is set at the upper port of material distribution pipe, tube wall trepanning is arranged in part of the material distribution pipe between upper tower tray and lower tower tray, recycle oil reactor inlet is also set up between upper tower tray and lower tower tray；The utility model flows back into the solid catalyst that three phase separator separates in reactor in reactor radial center regional subsidence, when solving high catalyst loadings, the big problem of resistance of catalyst sedimentation reflux ensure that three phase separator still has good separating effect in high catalyst loadings.
Description
Technical field
The utility model is related to ebullated bed technical fields, and in particular to a kind of fluidized bed reactor.
Background technology
Boiling bed hydrogenation reaction refers to feedstock oil (predominantly liquid phase), hydrogen (gas phase) carries out adding hydrogen on catalyst (solid phase)
The process of reaction, hydrogenation reaction mainly occur hydrodesulfurization, hydrodenitrogeneration, hydrogenation deoxidation plus hydrogen and are saturated, are hydrocracked.Instead
Device is answered to be operated under the fluidized state of gas, liquid, solid three-phase, catalyst is in the feedstock oil entered from reactor bottom and the band of hydrogen
Under dynamic, it is in fluidized state, entirely different fluid state is in fixed bed reactors.Boiling bed hydrogenation reaction can be handled
The inferior feedstock oil of high metal, high asphalt content, reaction is small with pressure drop, temperature is uniform, can add row's catalyst online,
The features such as to keep catalyst activity.
The material of fluidized bed reactor is introduced from reactor bottom, and gas-liquid distribution is generally arranged in the lower part in reactor
Device, material is evenly dispersed.Gas-liquid point this orchestration is generally tray type structure, be arranged on disk material by distribution pipe, distribution
The setting of tube top portion intercepts the calotte of catalyst granules.Since the raw material of ebullated bed processing is generally poor heavy raw material, feature
It is to be easy to coking, therefore be easy to coking and blocking on fluidized bed reactor gas-liquid allotter, existing method is usually to distributor
Surface carries out special disposal, and coking material is made to be not easy to be attached on gas-liquid allotter.
Presently, there are two kinds of major type of boiling hydrogen addition technologies, one kind is such as USRe25 by the way of oil phase cycle,
Boiling bed process described in 770, the deficiency of this technique in practical applications are：To keep solid-liquor separation effect, reactor
Interior catalyst amount cannot be too many, and reactor utilization rate is low, industrial fluidized bed reactor utilization rate generally only 40% or so, profit
Refer generally to the percentage that loaded catalyst accounts for reactor volume (disregarding end socket space), fixed bed reactors utilization rate one with rate
As 90% or more；It is that residence time of the liquid material under no catalytic condition is long that reactor, which has larger space, this position does not have
There are hydrogenation reaction, material to be easy reaction coking at high temperature.Another kind of is that three phase separator is arranged in reactor, in reactor
Internal upper part carries out gas-liquid-solid separation can improve the dosage of catalyst by three phase separator built in setting, that is, improve reaction
Device utilizes space, but in actual use, and catalyst amount raising is limited, if catalyst amount increases, three phase separator
Separating effect rapid decrease, actually than first kind fluidized bed reactor utilization rate slightly improve；Another improvement project is
In three phase separator lower part, setting guide frame increases the operating flexibility of three phase separator, it is ensured that three-phase separate using guide frame
From efficiently separating for device, the drag-out of catalyst is reduced, improves catalyst inventory, improves reactor utilization rate, but when in use,
It still needs to that catalyst lean phase region is arranged in the certain area in three phase separator lower part, the region catalytic amount is seldom, does not occur to add hydrogen substantially
Reaction, otherwise the separating effect of three phase separator cannot still be met the requirements, and the presence of dilute-phase zone, influence reactor utilization rate
It is further promoted, also influences hydrogenation reaction effect, and after the amplification of reactor scale, catalyst loading is more difficult to improve, it is difficult to
Achieve the effect that experimental provision.Although the latter is theoretically not required to recycle oil, go into operation, stop work, operation exception when can cause to urge
Agent is difficult to reach stable fluidized state, and operational stability is insufficient.Therefore, the utilization of boiling bed hydrogenation reactor how is improved
Efficiency improves reaction effect, improves the stability of device, be this field technical issues that need to address.
In addition, the factor for influencing three phase separator separating effect in the anti-device of ebullated bed is not only in that the knot of three phase separator
Structure, material system status, also have much relations with earth rotation.Gas, liquid, solid three-phase state in the anti-device of ebullated bed, gas, liquid are whole
Body is in the state that flows up, and solid catalyst is in boiling quick condition.Earth rotation has above-mentioned material state certain
Active force, form slight cyclonic action, in the larger reactor of industry, due to larger, this cyclonic action is more
Show.As a result, catalyst, in the region clustering close to reactor wall, reactor radial center region is more sparse.It is this
Effect produces the separating effect of existing three phase separator and significantly affects, i.e., when loaded catalyst increases, three phase separation
The solid catalyst that device is separated settles back the increase of the resistance in reactor, and the chance for being taken out of reactor by liquid material carries
Height makes reactor take catalytic amount increase out of, influences reaction effect.
Utility model content
In order to solve the above-mentioned technical problem the deficiency in, the purpose of this utility model is that：A kind of ebullating bed reactor is provided
Device can effectively solve the coking problem of gas-liquid allotter, can further increase the utilization rate of reactor, that is, improve reactor
Interior catalyst inventory can further promote hydrogenation reaction effect, improve the stability of device operation.
The utility model is that technical solution used by solving its technical problem is：
The fluidized bed reactor, including reactor shell, the upper end of reactor shell are respectively set catalyst and mouth are added
And material inlet and catalyst outlet is arranged in gas vent, the lower end of reactor shell, the upside inside reactor shell is set
Set three phase separator, downside inside reactor shell is arranged gas-liquid allotter, the gas-liquid allotter include material distribution pipe,
Upper tower tray and lower tower tray, upper tower tray and lower tower tray form the double-deck tray structure, and gap, material are formed between upper tower tray and lower tower tray
Distribution pipe runs through upper tower tray and lower tower tray, is arranged calotte at the upper port of material distribution pipe, material distribution pipe be located at upper tower tray with
Tube wall trepanning is arranged in part between lower tower tray, and recycle oil reactor inlet is also set up between upper tower tray and lower tower tray.
Preferably, three phase separator includes inner barrel and outer barrel, and inner cylinder is arranged in the inside of outer barrel, the concentric setting of the two,
The upper and lower ends of the inner barrel and outer barrel are all open, and the upper end opening of outer barrel is less than the upper end opening of inner cylinder, under outer barrel
End opening is less than the lower ending opening of inner cylinder.
Preferably, setting cycle oil system between three phase separator and gas-liquid allotter, cycle oil system includes recycle oil
Pump and recycle oil pipeline, the entrance of recycle oil pipeline are arranged in the liquid phase region of three phase separator, the outlet of circulation line and gas-liquid
Recycle oil reactor inlet connection on distributor.
Preferably, outer barrel is divided into direct tube section and contraction section, and contraction section is taper type.
Preferably, baffle is arranged in the lower section of outer barrel.
Preferably, baffle is spindle baffle.
Preferably, to be tightly connected between material distribution pipe and upper tower tray and lower tower tray, tube wall trepanning is annular opening.
Preferably, the tube wall trepanning number being arranged in every material distribution pipe is 3-7, uniform in material distribution pipe one week
Setting.
Compared with prior art, the utility model has the advantages that：
1, the solid catalyst that the utility model separates three phase separator is in reactor radial center regional subsidence
It flows back into reactor, when solving high catalyst loadings, the big problem of resistance of catalyst sedimentation reflux ensure that three-phase separate
Still there is good separating effect in high catalyst loadings from device.
2, the utility model can further increase loaded catalyst ratio, especially large-scale industry ebullating bed reactor
The Catalyst packing ratio of device reduces or eliminates catalyst lean phase region while improving reactor volume utilization rate, is promoted
Hydrogenation reaction effect.
3, the newly-designed three phase separator of the utility model overcomes catalyst distribution unevenness caused by earth rotation and causes
Influence reaction effect the problem of.
4, gas-liquid allotter coking phenomenon is substantially reduced, and is not easy the coking on gas-liquid allotter, and the protective layer of formation makes newly
Fresh raw material is not in direct contact with gas-liquid allotter, is effectively prevented fresh feed coking material and is adhered on gas-liquid allotter, in turn
Avoid the blocking of gas-liquid allotter.
Description of the drawings
The structural schematic diagram of Fig. 1 the utility model；
The structural schematic diagram of Fig. 2 the utility model gas-liquid allotters.
In figure：1, gas vent；2, liquid outlet；3, reaction liquid effluent piece-rate system；4, oil circulating pump；5, it is catalyzed
Agent outlet；6, material inlet；7, reactor feed system；8, gas-liquid allotter；9, reactor shell；10, baffle；11、
Outer barrel；12, inner cylinder；13, mouth is added in catalyst；14, calotte；15, upper tower tray；16, recycle oil reactor inlet；17, tube wall is opened
Hole；18, material distribution pipe；19, lower tower tray.
Specific implementation mode
The utility model embodiment is described further below in conjunction with the accompanying drawings：
Embodiment 1
As shown in Figs. 1-2, fluidized bed reactor described in the utility model, including reactor shell 9, reactor shell 9
Upper end is respectively set catalyst and mouth 13 and gas vent 1, the lower end setting material inlet 6 and catalyst of reactor shell 9 is added
Three phase separator is arranged in outlet 5, the upside inside reactor shell 9, the downside setting gas-liquid distribution inside reactor shell 9
Device 8, the gas-liquid allotter 8 include material distribution pipe 18, upper tower tray 15 and lower tower tray 19, and upper tower tray 15 and lower tower tray 19 are formed
The double-deck tray structure of the double-deck tray structure, gas-liquid allotter 8 is tightly fixed on the inner wall of reactor shell 9, upper tower tray
Form gap between 15 and lower tower tray 19, material distribution pipe 18 runs through upper tower tray 15 and lower tower tray 19, material distribution pipe 18 it is upper
Calotte 14 is set at port, tube wall trepanning 17 is arranged in part of the material distribution pipe 18 between upper tower tray 15 and lower tower tray 19,
17 numbers of the tube wall trepanning being arranged in every material distribution pipe 18 are 3-7, preferably 6, uniform in material distribution pipe 18 1 weeks
Setting, recycle oil reactor inlet 16 is also set up between upper tower tray 15 and lower tower tray 19.
Three phase separator is divided into three phase regions of gas, liquid, solid, and three phase separator includes inner cylinder 12 and outer barrel 11, and inner cylinder 12 is set
It sets in the inside of outer barrel 11, the concentric setting of the two, the upper and lower ends whole opening of the inner cylinder 12 and outer barrel 11, inner cylinder 12
Liquid phase region liquid outlet 2 is set, the upper end opening of outer barrel 11 is less than the upper end opening of inner cylinder 12, and the lower ending opening of outer barrel 11 is low
In the lower ending opening of inner cylinder 12, outer barrel 11 divides for direct tube section and contraction section, and contraction section is taper type, the lower ending opening of the contraction section
That is the lower ending opening of outer barrel 11；It is arranged suitable for gap, in order to material between 11 contraction section of lower ending opening and outer barrel of inner cylinder 12
Pass through, baffle 10 is arranged in the lower section of 11 lower ending opening of outer barrel, and baffle 10 is spindle baffle 10, and spindle is axially transversal
Face maximum diameter is generally 1~3 times of 11 lower ending opening diameter of outer barrel；The three phase separator and reactor shell 9 are same
Axle center is arranged, and the outer barrel 11 of three phase separator can be fixed on by support construction on 9 inner wall of reactor shell, three phase separator
Inner cylinder 12 can be fixed on by support construction on 11 inner wall of outer barrel；On three phase separator top, gas phase is empty for gas phase zone setting
Between be highly the 0~20% of reactor shell 9 (do not include reactor end socket part), preferably 5%~10%.
Setting cycle oil system between three phase separator and gas-liquid allotter 8, cycle oil system include oil circulating pump 4 and follow
Ring oil pipe line, oil circulating pump 4 are arranged on circulating pipe road, provide power, and the entrance of recycle oil pipeline is arranged in three phase separation
The liquid phase region of device, the outlet of circulation line are connected to the recycle oil reactor inlet 16 on gas-liquid allotter 8, gas-liquid allotter 8
Recycle oil is introduced from the tube wall trepanning 17 of material distribution pipe 18, the protection of recycle oil is formed in 18 inner wall of material distribution pipe
Layer.Recycle oil is the material by hydrogenation reaction, and coking tendency is substantially reduced, and is not easy coking on the dispenser, the protection of formation
Layer makes fresh feed be not in direct contact with gas-liquid allotter 8, effectively prevents fresh feed coking material and adheres on the dispenser, into
And avoid the blocking of distributor.
Wherein, to be tightly connected between material distribution pipe 18 and upper tower tray 15 and lower tower tray 19, tube wall trepanning 17 is ring
Shape is open, and annular opening is the annular opening around entire 18 circumference of material distribution pipe, can also be in 18 circumference of material distribution pipe
The annular opening of upper setting unit, at this point, being preferably uniformly arranged along material distribution pipe 18.The design parameter of gas-liquid allotter 8 can
To carry out conventional design according to reactor scale.
In addition, fluidized bed reactor described in the utility model can be arranged as required to other components, as reactor into
Material system 7, system for detecting temperature, pressure detecting system, fluid flow state detecting system, is urged at reaction liquid effluent piece-rate system 3
The one or more such as agent distribution detecting system, material reallocation system；Fluidized bed reactor can be arranged as required to
Corollary apparatus, such as raw material pump, heat exchanger, heating furnace, separator.
In the utility model, the diameter of the 11 top direct tube section of outer barrel of three phase separator is general in boiling bed hydrogenation reactor
It is the 50%~90% of 9 internal diameter of reactor shell, preferably 75%~85%.Annular space distance one between inner cylinder 12 and outer barrel 11
As be 11 corresponding position radius of outer barrel 30%~70%, preferably 40%~60%.12 upper end of inner cylinder and 11 upper end of outer barrel
Difference in height is generally the 10%~50% of 11 radius of outer barrel, and preferably 20%~40%.The lower ending opening of inner cylinder 12 and outer barrel 11
Gap between contraction section is generally the 5%~40% of 11 direct tube section radius of outer barrel, and preferably 10%~30%.Outer barrel 11 is shunk
Section lower ending opening diameter is generally the 10%~50% of 11 direct tube section diameter of outer barrel, preferably 15%~35%.11 lower part of outer barrel
The angle of throat (acute angle of direct tube section and taper type contraction section) of taper type contraction section is 20 °~80 °, preferably 30 °~60 °.
The height of 11 top direct tube section of outer barrel is generally 0.4~3m, preferably 0.5~1m.
The utility model boiling bed hydrogenation method, using the boiling bed hydrogenation reactor of the utility model, reaction raw materials can
With heavy, inferior raw material, such as decompression residuum, coal tar, liquefied coal coil, asphalt oil sand, shale oil.Catalyst is generally solid
Particle, particle diameter are generally 0.6~2mm (in terms of isometric spherical shape), catalyst generally using aluminium oxide as carrier, with Mo, W,
Ni, Co etc. at least one are active component, while can add related auxiliaries.Catalyst is in 9 interior loading amount of reactor shell (with quiet
Only state meter) it is the 50%~85% of reactor volume, preferably 65%~80%, most preferably 72%~78%.React item
Part can require to determine according to feedstock property and reaction depth, General reactions pressure is 5~25MPa, reaction temperature be 200~
500 DEG C, hydrogen is 300~2000 with feedstock oil standard state lower volume ratio, feedstock oil and catalyst volume (stationary state) phase
The volume space velocity of ratio is 0.1~2h-1。
In the utility model boiling bed hydrogenation method, oil system is recycled by the Matter Transfer of three phase separator liquid phase region to gas
Liquid distributor 8, according to reaction conversion ratio, feedstock property, catalyst performance etc., specifically experiment determines internal circulating load, generally feedstock oil
The 10%~100% of amount.
Through experiment, it is fresh feed to control and be recycled back to the cycle oil mass of reactor shell 9 from the phase region of three phase separator liquid
30%, through 3000 hours long term tests, gas-liquid allotter 8 was without apparent coking phenomenon.
Embodiment 2
On the basis of embodiment 1, three phase separator separating effect carries out simulated experiment using chill.The ruler of cold model unit
It is very little to be：The internal diameter 200mm of reactor shell 9, the height 3500mm of reactor shell 9, three phase separator height 400mm, three-phase
The diameter 300mm of the 11 top direct tube section of outer barrel of separator, the annular space distance between inner cylinder 12 and outer barrel 11 is 80mm, inner cylinder 12
The difference in height of upper end and 11 upper end of outer barrel is 60mm, and the gap between 11 contraction section of lower ending opening and outer barrel of inner cylinder 12 is
60mm, the 11 a diameter of 90mm of contraction section lower ending opening of outer barrel, angle of throat (direct tube section and the cone of 11 lower part taper type contraction section of outer barrel
The acute angle of platform shape contraction section) 35 °.The 10 a diameter of 150mm of spindle axial cross section maximum of baffle.Using kerosene as
Liquid, oil inlet quantity are 60~120L/hr；It is 2~4Nm that gas phase, which selects nitrogen, air inflow,3/hr.Solid phase select grain size be 0.7~
The aluminum oxide micro-sphere catalyst of 0.8mm, catalyst inventory (in terms of when static) are reactor dischargeable capacity (disregarding end socket space)
55%~80%.
Test result see the table below.
1 cold model unit test result of table
From cold model experiment as can be seen that the utility model have good solid separating effect, applicable operating range compared with
Extensively.
The above is only the preferable case study on implementation of the utility model, is not to make other shapes to the utility model
The limitation of formula, any person skilled in the art are changed or are modified as possibly also with the technology contents of the disclosure above
With the equivalent embodiment of variation.But every without departing from the content of the technical scheme of the utility model, the technology according to the utility model
Essence still falls within technical solutions of the utility model to any simple modification, equivalent variations and remodeling made by above example
Protection domain.
Claims (8)
1. a kind of fluidized bed reactor, including reactor shell (9), the upper end of reactor shell (9) are respectively set catalyst and add
Entrance (13) and gas vent (1), the lower end setting material inlet (6) and catalyst outlet (5) of reactor shell (9), instead
Answer the upside setting three phase separator that device cylinder (9) is internal, which is characterized in that gas is arranged in the internal downside of reactor shell (9)
Liquid distributor (8), the gas-liquid allotter (8) include material distribution pipe (18), upper tower tray (15) and lower tower tray (19), upper tower tray
(15) and lower tower tray (19) forms the double-deck tray structure, and gap, material distribution are formed between upper tower tray (15) and lower tower tray (19)
It manages (18) and runs through upper tower tray (15) and lower tower tray (19), calotte (14), material point are set at the upper port of material distribution pipe (18)
It is piped the part setting tube wall trepanning (17) of (18) between upper tower tray (15) and lower tower tray (19), upper tower tray (15) He Xiata
Recycle oil reactor inlet (16) is also set up between disk (19).
2. fluidized bed reactor according to claim 1, which is characterized in that three phase separator includes inner cylinder (12) and outer barrel
(11), inner cylinder (12) setting is in the inside of outer barrel (11), the concentric setting of the two, the inner cylinder (12) and outer barrel (11) it is upper
Lower both ends are all open, and the upper end opening of outer barrel (11) is less than the upper end opening of inner cylinder (12), and the lower ending opening of outer barrel (11) is low
Lower ending opening in inner cylinder (12).
3. fluidized bed reactor according to claim 1, which is characterized in that three phase separator and gas-liquid allotter (8) it
Between setting cycle oil system, cycle oil system includes oil circulating pump (4) and recycle oil pipeline, and the entrance of recycle oil pipeline, which is arranged, to exist
The liquid phase region of three phase separator, the outlet of circulation line are connected to the recycle oil reactor inlet (16) on gas-liquid allotter (8).
4. fluidized bed reactor according to claim 2, which is characterized in that outer barrel (11) is divided into direct tube section and contraction section,
Contraction section is taper type.
5. fluidized bed reactor according to claim 2 or 4, which is characterized in that baffle is arranged in the lower section of outer barrel (11)
(10)。
6. fluidized bed reactor according to claim 5, which is characterized in that baffle (10) is spindle baffle.
7. fluidized bed reactor according to claim 1, which is characterized in that material distribution pipe (18) and upper tower tray (15) with
And to be tightly connected between lower tower tray (19), tube wall trepanning (17) is annular opening.
8. fluidized bed reactor according to claim 1 or claim 7, which is characterized in that be arranged on every material distribution pipe (18)
Tube wall trepanning (17) number be 3-7, be uniformly arranged within (18) one weeks in material distribution pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820188715.8U CN207929188U (en) | 2018-02-02 | 2018-02-02 | fluidized bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820188715.8U CN207929188U (en) | 2018-02-02 | 2018-02-02 | fluidized bed reactor |
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| Publication Number | Publication Date |
|---|---|
| CN207929188U true CN207929188U (en) | 2018-10-02 |
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ID=63651176
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820188715.8U Active CN207929188U (en) | 2018-02-02 | 2018-02-02 | fluidized bed reactor |
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| Country | Link |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108067169A (en) * | 2018-02-02 | 2018-05-25 | 上海英保能源化工科技有限公司 | fluidized bed reactor |
| CN111942832A (en) * | 2019-05-16 | 2020-11-17 | 松下知识产权经营株式会社 | Powder supply device |
-
2018
- 2018-02-02 CN CN201820188715.8U patent/CN207929188U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108067169A (en) * | 2018-02-02 | 2018-05-25 | 上海英保能源化工科技有限公司 | fluidized bed reactor |
| CN108067169B (en) * | 2018-02-02 | 2023-09-15 | 上海竣铭化工工程设计有限公司 | Ebullated bed reactor |
| CN111942832A (en) * | 2019-05-16 | 2020-11-17 | 松下知识产权经营株式会社 | Powder supply device |
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| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20181019 Address after: 200120 104, room 1, 2555 Xiu Pu Road, Pudong New Area, Shanghai. Patentee after: Shanghai Jun Ming Chemical Engineering Design Co. Ltd. Address before: 201400 1278, room 6, 1150 LAN Feng Road, Fengxian District, Shanghai. Patentee before: SHANGHAI YINGBAO ENERGY CHEMICAL TECHNOLOGY CO., LTD. |
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| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190401 Address after: 200120 104, room 1, 2555 Xiu Pu Road, Pudong New Area, Shanghai. Co-patentee after: LANZHOU LS HEAVY EQUIPMENT CORPORATION LTD. Patentee after: Shanghai Jun Ming Chemical Engineering Design Co. Ltd. Address before: 200120 104, room 1, 2555 Xiu Pu Road, Pudong New Area, Shanghai. Patentee before: Shanghai Jun Ming Chemical Engineering Design Co. Ltd. |
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| TR01 | Transfer of patent right |